Procedure for extraction of nickel and cobalt out of laterite ore

FIELD: metallurgy.

SUBSTANCE: procedure consists in leaching at atmospheric or raised pressure, in production of effluent and in utilisation of ion-exchanging resins for absorption and extraction of nickel and cobalt. Before extraction of nickel and cobalt effluent in form of solution or pulp is treated with cation or chelate resin possessing selectivity relative to extraction of iron, aluminium and copper for their removal; it also increases pH of solution.

EFFECT: elimination of neutralisation stage of solution, efficient purification of effluent, prevention of nickel losses and avoiding division of solid and fluid phase of formed pulp at laterite ore leaching.

6 cl, 2 dwg

 

Detailed description of the invention

The present invention is directed to a combined method using ion-exchange resins for the selective extraction of Nickel and cobalt from effluents leaching, consisting in at least two stages using resins, more specifically, to a combined cycle of two stages with the use of resin, where at the first stage of using the resin from solution remove iron, aluminum and copper, as well as increase the pH of the solution, and the second stage using resin extract Nickel and cobalt.

As is well known to specialists in this field, for the extraction of Nickel and cobalt present in lateritic ores have created several hydrometallurgical processes.

Their goal is to make the solubility of the metal particles by the use of inorganic acid to leach into piles or storage tanks at atmospheric pressure and temperature, which is below the boiling point, or in containers under pressure. The resulting solution then passes the stage of neutralization (removal of copper, iron, aluminum), the separation into solid and liquid phases (possible) and at least one purification step of the solution and the final metal recovery or intermediate product.

Selective extraction of metal present in affluence leaching is important from an economic point of view stage. The presence of many impurities, such as copper, iron, aluminum, manganese and magnesium, among other things, can be viewed as the main technological challenge that must be overcome.

One option may include physico-chemical methods, such as the use of ion-exchange materials, selective precipitation and solvent extraction. With specific regard to Nickel and cobalt, these metals have very similar chemical properties, which facilitates their joint extraction or by deposition in the form of a mixture of sulfides or mixtures of the hydroxides, or by solvent extraction in a chloride environment, or, finally, by the use of ion-exchange material such as polymer resin.

Ion exchange can be defined as the reversible exchange of ions between the solid phase and aqueous electrolyte so that the structure of the solid phase does not change significantly. In this case, the solid phase is an ion exchange material, which may be either inorganic nature, as, for example, zeolites or organic nature, as materials based on synthetic polymer resins. The matrix resin is composed of high molecular weight, insoluble, irregular, macromolecular, and three-dimensional elastic hydrocarbon chains resulting from the copolymerization of styrene and DV is albenzae. In this matrix functional groups with positive and negative charge are strongly related (fixed ions)that is compensated at the expense of ions with opposite charge (counterions). They are free to move within the matrix and can be in stoichiometric quantities replaced by other ions with the same charge. The so-called coiny, in contrast, are ions that may be present in the ion-exchange material and have the same charge as the fixed ions. The main types of resins used in industry include cationic resin, which, depending on the degree of acidity of functional groups can be weak or strong acids, and anionic resins which, depending on the degree of basicity, can be strong or weak bases, and chelating resins. Some materials, which are called amphoteric capable and cationic, and anionic exchange.

Chelating resins have been developed for the selective extraction of transition metals such as Nickel and cobalt from solutions, they form with such cations is very stable chelate complexes or metal-containing heterocyclic chelates. These chelates can be defined as compounds in which the ring is the result of the formation of the coordination of communication between two or more parts of the molecule and it is metal.

Chelate resin can be regarded as typical representatives of the group of ion-exchange polymeric resins used in hydrometallurgy, which differ in the possibility of selective removal of heavy metals such as Nickel and cobalt from acidic aqueous solutions. These ion exchange materials are copolymers, functional groups which are linked by covalent bond and contain one or more donor atoms (Lewis base), capable of forming coordination with the majority of polyvalent cations of heavy metals (Lewis acid). Usually in the functional groups of the chelate resins include atoms such as nitrogen, oxygen, phosphorus and sulfur. Examples of chelating functional groups include amidoxime, aminophosphonate, carbamates, polyamine, pyridine, iminodiacetate and picolylamine. Coulomb and hydrophobic interactions also occur; however, their contribution to the selectivity towards metal ions compared with the interaction of Lewis acids and bases is relatively small. These resins, as a rule, can be regenerated acid solution (sulfuric or hydrochloric acid), reaching thus high efficiency.

I believe that the use of ion exchange resins is one of the technological capabilities of purification/extraction of metals in the environment. Appropriate methodologies are part of the technological schemes hydrometallurgical methods of processing Nickel laterite ores, a necessary component of which is the stage of leaching, and are a way to extract metal from ore. Technology with the use of resin can be used on those existing installations, where the way counter-current decantation (CCD), and if the setup project is under development, can be directly applied to efluentes leaching with the aim of reducing costs and negative impacts on the environment.

The leaching can be carried out using acidic or basic leaching agent, in piles or storage tanks at atmospheric conditions, or in tanks under pressure. After extracting metal from ore and dissolution in aqueous solution to effluent leaching, having the form of a slurry or solution may be applied using ion-exchange resin, mainly chelate type, with the purpose of extraction of Nickel and cobalt.

To apply such processing with the use of polymer resins for the selective absorption of Nickel is possible in two ways, i.e. either to the resin solution or resin-in-pulp.

In the first case, the solution with dissolved metals filter, the example through the fixed layer of the resin so that it happened absorption, whereas in the second case, the pulp of the ore directly brought into contact with the resin under stirring so that the absorption of the metal occurred in the absence of the expensive stage of separation of the slurry into solid and liquid phases. After bringing it in contact with the resin is separated from the pulp by screening.

In the flow charts of processing of Nickel laterite ore acceptable either of these two options. To use the resin in the solution is a necessary preliminary stage separation of solid and liquid phases. At this stage, in addition to significant operating expenses and capital expenditures required extensive area and supply a large amount of water, and we have the loss of Nickel due to the inefficiency of the method, that is, because of the difficulty of washing the solid phase extraction of dissolved substances. For this reason, in many cases, it is proposed to apply the method using ion exchange resin to the pulp, as with the ion exchange material is extracted metal dissolved in the leaching actually in the pulp, and, thus, does not require separation of solid and liquid phases.

If the method using ion exchange resin in the pulp is used to extract Nickel from a solution of acid videl is zivania, can be obtained the following advantages: 1) the use of conventional resins, which are also selective with respect to iron, requires the prior, before removing Nickel neutralization. The iron hydroxide is easily precipitated by adding lime or limestone and becomes part of the pulp. 2) the Acidity of the pulp, as a rule, neutralize actually at the stage of absorption in the contact time with the resin. Can be used such reagents as lime or limestone, formed by neutralizing the suspension becomes part of the pulp. 3) as a result of acid leaching, followed by neutralization is formed or pulp, with difficulty settling, or solid phase, which is when the separation is difficult to wash out. When using resin-in-pulp of these difficulties can be avoided by eliminating phase separation of solid and liquid phases. 4) In this way is the phenomenon of sorption-leaching, since the contact part is precipitated by neutralizing Nickel leached again and, when he goes back into solution immediately absorbed by the resin. Thus, the use of resin-in-pulp allows you to minimize such losses and to extract about 20% Nickel, which had previously been co-deposition.

Ion exchange is a technology that has been perfected from different points of view, h is about was accompanied by very promising results. Ion exchange technology using polymer resins find application in industry in the flow charts of processing Nickel ore, has provided a number of advantages, such as no loss of reagents, the usual process for solvent extraction, efficient extraction and removal of small concentrations of some metal ions with an excess of other metals, high selectivity to the target metals, higher performance division, the flexibility of technological regimes, the simplicity of the technological scheme, obtaining a product of high purity with a high concentration of target metal on the concentration of impurities, a high level of automation. These characteristics allow to reduce operating costs and capital expenditures, as well as to reduce the impact on the environment by reducing water consumption and opportunities to recycle water.

Despite all the advantages mentioned above, the conventional resins, commercially available for the selective extraction of Nickel in the processing of laterite ore, is a new industrial technology, still has some limitations and operational interference.

One of the drawbacks, which can be specified in this document, is that the pH of the solution, which is a function of high is th selectivity with respect to hydrogen ions, should be increased to values greater than pH 3.0. Only in this case, conventional resins may be selective with respect to Nickel and implement the uptake of this metal. Otherwise, in the presence of an excess of hydrogen ions (low pH) will be their preferred absorption, which prevents the absorption of Nickel.

Another significant disadvantage is that the solution is in General formed by acid leaching of Nickel ore, in addition to Nickel and cobalt dissolved many metals, called impurities. Since many resins, selective with respect to Nickel, selective with respect to iron, copper and aluminum, the necessary pre-processing stage solution, which removes these impurities.

There are already technologies proposed in an attempt to solve the aforementioned problems, for example the implementation stage neutralization immediately after leaching by adding lime, limestone, soda or ammonia in order to precipitate the impurities and simultaneously increase the pH.

Although this is very effective from the point of view of overcoming technical limitations, such as excessive acidity of the solution and the presence in the solution of the impurities, the neutralization associated with the presence of such drawback as significant loss of Nickel deposited together with impurities.

Another disadvantage observed is when neutralization, is the need for expensive phase separation of solid and liquid phases in case, if you choose to use the resin in solution.

In both cases, the application of the resin in solution and in the pulp, in fact, a necessary preliminary stage of neutralization of acidity, which increase pH and remove impurities by sedimentation, as shown in the flowsheet of the process lateritic ore, is shown in figure 1. In this process, the necessary stage of neutralization, however, it entails significant, the already mentioned disadvantages, such as loss of Nickel deposited together with the impurities, and the need for phase separation of solid and liquid phases, if you choose to use the resin in solution.

It is important to note that the use of resin-in-pulp, though, and provides all the above mentioned advantages, it still has some limitations and is associated with technical risk, such as lack of resin having high mechanical strength and abrasive wear resistance, sufficient for contact with the pulp. For this reason, for a long time it was believed that the use of resin in the solution is the best option and, thus, the ore was subjected to pre-treatment with all the attendant disadvantages, such as loss of Nickel in the deposition, with subsequent costly the stage of separation of solid and liquid phases.

This problem is greatly compounded if the leaching is carried out in heaps. Effluent formed after this operation, ready for submission to the machining stage resin in solution. This clarified solution not containing solid particles, which, therefore, suitable for submission to the fixed layer of resin, for example, in the column. The need for pre-processing stage creates a number of difficulties, such as the formation of the pulp with the inevitable loss of Nickel from the sediment, which then need to be divided into solid and liquid phases, after which the clarified water is fed to the column of ion exchange.

The present invention therefore is to propose a combined method using ion exchange resin, which is excluded stage neutralization (pre-processing) solution.

Another objective of the present invention is to propose a combined method using ion-exchange resins which can be cost-effective cleaning effluent leaching.

Another objective of the present invention is to propose a combined method using ion exchange resin, which prevents the loss of Nickel from the sediment in the co-deposition.

Another objective of the present invention is to propose combo receiver who spent the method of using ion exchange resin, at which eliminates the separation of the solid and liquid phases of the resulting pulp.

These and other objectives and advantages of the present invention are achieved by a method, which uses an ion-exchange resin, which includes an additional first processing cycle cationic resin, mobile ions which are preferably alkali metal ions, with the intent of increasing the pH of the solution and absorption of impurities. Combined method of ion exchange includes the first stage of ion exchange with resins under certain conditions, the selectivity to remove iron, aluminum and copper and raise pH and the second stage ion exchange, preferably with the use of resins iminodiethanol group, which can extract Nickel and cobalt.

Hereinafter the present invention will be described with reference to the accompanying drawings, where:

figure 1 is a flow diagram of the conventional method of extraction of Nickel from lateritic ores;

figure 2 is a flow diagram of a combined method including two loop ion exchange resins for selective extraction of impurities in the first stage and selective extraction of Nickel and cobalt from effluent leaching in the second stage.

It should be noted that the resin (picolylamine groups who), which can absorb Nickel in a very acidic environment and the presence of impurities in high concentrations on the market, however, its value for most cases of extraction of Nickel is extremely high. In the method proposed in this document, this resin is not required, because there is no need to pre-treatment: no in the removal of impurities, even in the increase of pH, therefore, there are no disadvantages associated with the specified stage.

According to available figures, the proposed solution is to exclude the pre-treatment (neutralization) of the slurry to increase the pH and precipitation of impurities, such as iron, aluminum and copper, thereby preventing loss of Nickel from the sediment in the co-deposition and eliminates the necessity of separating the resulting slurry into solid and liquid phase.

The present proposal is to organize a two-stage combined cycle using ion exchange resin, where the resin may be the same or different, different types, with different functional groups and from different manufacturers. Two stage ion-exchange resins are applied to the solution coming from the stage of separation of solid and liquid phases of existing facilities, or to effluent wimalasiri the planned facilities, containing dissolved metals, including high concentrations of iron, aluminum, manganese and magnesium, in addition to Nickel, cobalt and copper.

As can be seen from the process flowsheet shown in figure 2, the combined method using ion-exchange resins begins the same way, as usual, that is, the processing (1) laterite ore (M). Ore (M) after treatment (1) subjected to leaching (2) (at atmospheric or increased pressure, or combination), or also can be the case a solution after separation of solid and liquid phases in the existing unit (2).

It is expected that effluent (E1) after such processing is acidic (pH<2) and does not require processing at the preliminary stage (i), as occurs in the conventional way. The first stage (3) cationic ion exchange combined cycle, in which the mobile ions of the resin must be ions of alkaline metals in the disodium form, leads to the increase of pH. The purpose of this phase is the removal of impurities, such as iron, copper and aluminum, therefore, the resin (Re) should preferably absorb iron, copper and aluminum under conditions of high acidity, which are affluence (2) Nickel ore (M).

The aim of the first stage of ion exchange (3) is the extraction of iron, copper and aluminum and separation of Nickel and to the of Balta. In order for this to happen effectively, the pH of the solution/slurry supplied to this stage should be low (lower than pH of 2.5), similar to the conditions found in affluence (E1) after leaching (2) laterite ores (M). Under these conditions, and using a suitable cationic or chelate resin impurities (iron, copper and aluminum) should be absorbed by the resin (Re) and, thus, be removed, at the same time, Nickel and cobalt are separated and remain in solution. The use of resin, regenerated with alkali metal ions, for example, disodium form, is very significant, because these mobile ions are replaced by ions of Fe3+Al3+and Cu2+therefore, ions of alkali metals into solution, raising the pH. Role nature of the alkali metal ions present in the solution, is to increase the pH of the solution so that the solution could apply for the second stage processing using ion-exchange resins with a higher pH.

The second stage (4) ion exchange, following the first, which serves affluent (E2) with the first stage (3), is used to extract Nickel and cobalt from solution under more mild conditions of pH and without interference from impurities. For this to happen effectively, the pH of the solution should be greater than 1, preferably, as close to a 4.0 as uh what about the possible what is achieved by moving in a solution of alkali metal ions during the exchange extraction in the first stage. If you need to raise pH at the intermediate stage between stages 1 and 2 can be used reagent basic nature. Under the conditions created in the second stage, the chelate resin (Re), preferably having a functional group iminodisuccinic acid, which is considered suitable from the point of view of cost, still shows high selectivity with respect to iron, aluminium and copper. Since these impurities have already been removed from the solution at the previous stage, the resin (Re) in the second stage (4) is in the best conditions from the point of view of efficient and selective extraction of Nickel and cobalt.

Operating conditions of these two stages, conditions such as pH of the medium, the dimensions of the equipment, time and operational capabilities must be different. At both stages may be used the same resin (Re), it is also possible to use two different resins (Re) in accordance with the characteristics of the treated solution. If you decide to use the same resin (Re), this is a very reasonable choice, which is the most recommended.

After the second stage (4) the method involves the same stages as the usual way, that is, the resin (Re) absorbed ions of cobalt and Nickel is subjected to the leaching (5), namely, the resin (Re) is brought into contact with solvents, such as hydrochloric or sulfuric acid, or any salt of ammonium, resulting metals are separated from the resin (Re), which is then recovered and again sent to the loop at the second stage (4). After washout (5), if necessary, carry out the separation of Nickel and cobalt by solvent extraction (6), the extracted metals may be metal or any other mixed form.

Thus, the combined method of using ion exchange resins allows you to clean effluent leaching, in the form of a slurry or solution obtained, usually with some form of leaching of Nickel ores (M).

Although described and illustrated the preferred concept of this technical solution, it should be noted that other possible solutions are not beyond the scope of the present invention.

1. The method of extraction of Nickel and cobalt from lateritic ores, including leaching at atmospheric or elevated pressure to get affluent and the use of ion exchange resins to absorb and recover Nickel and cobalt, characterized in that before the extraction of Nickel and cobalt handle effluent taken in the form of a solution or slurry, cationic or chelate resin, with a selectivity to removing the ELISA, aluminum and copper for their removal and the ability to increase the pH of the solution.

2. The method according to claim 1, characterized in that effluent served on the extraction of iron, aluminum and copper, is acidic with a pH<2 and when using a suitable cationic or chelate resin admixture of iron, copper and aluminum are absorbed by the resin, and Nickel and cobalt remain in solution.

3. The method according to claim 1, characterized in that the resin under conditions of high acidity that is used at the stage of removal of iron, copper and aluminum, preferably absorbing iron, copper and aluminum, in addition, preferably contains mobile ions of alkali metals, for example, disodium form, which are replaced by ions of Fe3+, Al3+and Cu2+and thereby increase the pH of the solution.

4. The method according to claim 1, characterized in that between stage removal of iron, copper and aluminum and the stage of extraction of Nickel and cobalt spend intermediate stage of neutralization of a strong basic reagent to raise the pH and provide the necessary acidity conditions in afluente supplied to the stage of absorption of Nickel and cobalt.

5. The method according to claim 1, characterized in that at the stage of extraction of Nickel and cobalt stage after removal of iron, copper and aluminum are used cationic or chelate resin, preferably having iminodiacetate functional groups, the softer is the acidity conditions and without interference from impurities of iron, aluminum and copper, effectively and selectively absorptive of the solution of Nickel and cobalt.

6. The method according to claim 1, characterized in that after the stage of absorption of Nickel and cobalt resin containing ions of cobalt and Nickel, is subjected to leaching, regenerate inorganic solutions and again sent to the stage of absorption of Nickel and cobalt resin, and after washout carry out the separation of Nickel and cobalt by solvent extraction and extract the metals from the solution in the metallic form or another.



 

Same patents:

FIELD: metallurgy.

SUBSTANCE: procedure for extraction of scandium consists in extracting scandium out of producing sulphuric acid solution whereto alkali agent is added before extraction to bring its acidity to pH equal to 2.5-3.0 on solid extractant (SOLEX) with raised selectivity to scandium. Further, scandium is re-extracted from the SOLEX after complete extraction by processing it with solution of fluorine-hydrogen acid at ratio 1:3 of water and organic phases. Successively, scandium fluoride is settled and the SOLEX is washed. Before re-extraction the SOLEX is after-saturated with a part of concentrated solution of scandium produced from preceding re-extraction. Extraction and re-extraction are performed in the same sorption unit; spent sulphuric acid solution and the SOLEX washed with water are returned for extraction of scandium. The procedure for production of the SOLEX consists in synthesis of styrene-di-vinyl-benzene with di-2-ethyl-hexyl ether of phosphoric acid at presence of initiator of copolymerisation. As initiator there is used di-nitrile of azo-di-izobutyric acid to increase strength properties of granules of extractant at the following ratio, wt %: di-2-ethyl-hexyl ether of phosphoric acid - 40-60, di-nitrile of azo-di-izobutyric acid - 3-5, ammine-methyl-phosphonic acid - 3-5, styrene-di-vinyl-benzene - the rest. Produced mixture is poured with distilled water and heated at equal ratio of water and organic phases, overflowed through a sieve and rapidly cooled at continuous mixing with formation of porous granules of the SOLEX which are cut and dried.

EFFECT: efficient process for extraction of scandium.

4 cl, 1 tbl, 4 ex

FIELD: metallurgy.

SUBSTANCE: production of Mo-99 consists in filling solution reactor with fuel solution of uranyl-sulphate, in starting reactor up to specified power, in forming Mo-99 in fuel solution, in reactor shut-down, in conditioning fuel solution for decay of short-lived radionuclide and in sorption of Mo-99 from solution. Also, after reactor shut-down fuel solution is poured out of the reactor into at least one nuclear-safe reservoir; fuel solution is conditioned in this nuclear-safe reservoir. An empty reactor is repeatedly filled with fuel solution, is started up to specified power and Mo-99 is repeatedly generated in fuel solution. For the period of Mo-99 generation in the fuel reactor poured fuel solution in the nuclear-safe reservoir is conditioned. Mo-99 is sorbed from conditioned fuel solution by pumping it through at least one sorption column wherefrom Mo-99 is sorbed into at least one nuclear-safe reservoir for fuel solution conditioning. Fuel solution is conditioned, if necessary. Repeatedly emptied reactor is filled with fuel solution from the nuclear-safe reservoir for fuel solution conditioning.

EFFECT: raised efficiency of solution reactor producing Mo-99 under discrete mode due to reduced idle time.

9 cl, 1 dwg, 1 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in saturating pulp prepared from ore with oxygen and in introducing leaching reagents and sorbents. Further, there are performed sorption leaching with saturation of sorbent with metal impurities and partially with valuable metals, in counter-flow sorption of base part of valuable metals and in withdrawing sorbents saturated with valuable metals. Also, before introduction of leaching reagents activating solution, treated with light radiation in ultraviolet region of spectre or photo-electro-chemically treated, is introduced into pulp prepared out of ore containing valuable metals in dispersed form. Sorption leaching is carried out in electric field for electro-sorption extraction of primarily leached metals with periodic withdrawal of sorbent from zone of electro-sorbtion.

EFFECT: reduced losses of industrially valuable metals.

3 cl

FIELD: metallurgy.

SUBSTANCE: procedure consists in production of sample containing uranium and silicon dioxide, in treatment of sample containing uranium and silicon dioxide and in production of material containing dissolved uranium and silicon dioxide. Also, material contains SiO2 over or equal to 100 mg/l. Further, dissolved uranium is extracted from material using at least one strong base anion-exchanging resin of macro-reticular structure. There is obtained uranium containing product in combination with strong-base anion-exchanging resin of macro-reticular structure. Further, uranium containing product is eluted and extracted from combination with strong-base anion-exchanging resin of macro-reticular structure.

EFFECT: increased efficiency of uranium extraction from mediums with high contents of silicon dioxide.

9 cl, 3 tbl, 1 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in acid extraction of compounds of rare earth elements from phospho-gypsum by mixing extract suspension, in separation of insoluble sedimentation of crystal gypsum from extraction solution and in extracting compounds of rare earth elements from extraction solution. Also, acid extraction is performed with solution of mixture of sulphuric and nitric acids at ratio from 3.2 to 1.2 and concentration from 1 to 3 wt % at ratio L:S (liquid : solid) from 4 to 5 during 8-12 min with simultaneous hydro-acoustic effect onto mixed extraction suspension. Rare earth elements are extracted from extraction solution by means of cation-exchanging sorption with infiltration of extraction solution through cation-exchanging filter.

EFFECT: increased degree of extraction of rare earth elements and 2 times reduced time for process at lower concentrations and volumes of acid reagents.

3 cl, 2 tbl, 4 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in underground leaching nickel with solution of sulphuric acid and in pumping product solution out. Further, acidity of product solution is reduced, and nickel is sorbed on ionite resin with its following desorption. Upon desorption raffinate of nickel sorption is made-up with sulphuric acid and directed to leaching as leaching solution. Also, excessive sulphuric acid is sorbed on separate ionite with following desorption for reduction of product solution acidity. Upon nickel sorption raffinate is made-up with sulphuric acid and with sulphuric acid after operation of its desorption.

EFFECT: simplification of process, increased ecological safety and reduced consumption of sulphuric acid.

1 dwg, 1 tbl

FIELD: metallurgy.

SUBSTANCE: invention relates to method of extracting stibium from sulphate solutions. Proposed method comprises sorption on anionite and desorption of stibium from anionite by desorption solution. Sorption is carried out using Lewatit K 5517 anionite, while desorption is made via feeding desorption solution through stationary anionite layer at the rate of 0.35-0.46 m/h at 45-50C. Desorption solution represents disulphide alkaline solution with molar ratio S/NaOH=0.5 and/or alkaline solution of sodium sulphide with sodium concentration of at least 26 g/l.

EFFECT: stibium extraction and increased stibium concentration in solution intended for electrolysis.

3 dwg, 3 tbl

FIELD: metallurgy.

SUBSTANCE: invention relates to method of extracting stibium and arsenium from solution of gold-containing concentrate bioleach solutions. Proposed method comprises sorption of stibium and arsenium on anionite. Note here that sorption is performed on Lewatit K 5517 anionite, and stibium and arsenium are desorbed there from. Prior to desorption, anionite is subjected to sulphuric-acid washing out of iron deposit. Washing-out comprises rinsing by 1.2-1.3%-sulphuric acid with S:L ratio equal to 1:4 at 45-50C, flow rate of rinsing solution in anionite of 1.0-1.3 m/h, and dissolution of iron (III). Then, remaining iron (III) is washed out by 3%-solution of sodium sulphite at pH=1.5 and S:L=2.

EFFECT: higher yield of stibium and arsenium due to selective wags-out of iron for further desorption of them.

3 dwg, 1 tbl

FIELD: metallurgy.

SUBSTANCE: invention relates to the method of processing sulphide gold-containing concentrates. Proposed method comprises bioleach of concentrate involving stibium dissolution and extraction from solution by sorption. Note here that stibium sorption from bioleach solution is carried out on anionite Lewatit K 5517 at 45-50C, anionite flow rate making 50-100 g/l of solution for 8-10 hours. After sorption, desorption is carried out.

EFFECT: expanded process performances, increased extraction of stibium of gold-containing ores.

2 dwg, 1 tbl, 1 ex

FIELD: metallurgy.

SUBSTANCE: sorption method of rhenium (VII) from water solution involves contact of the solution and absorbent at pH<5. At that, activated bone coal pre-treated with water or acid is used as absorbent.

EFFECT: effective extraction of Re ions from water solution.

4 dwg, 3 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in leaching with chloride solution at supply of chlorine, in purification of solution from copper and in production of copper sulphide cake, in extracting concentrate of precious metals and in electro-extraction of nickel from solution. Prior to leaching matte is separated to a sulphide and metallised fractions. The sulphide fraction is subjected to leaching with chloride solution with supply of chlorine. The metallised fraction produced at separation of matte is added into pulp produced at leaching thus performing purification of solution from copper and its withdrawal to copper sulphide cake. Upon purification of solution from copper solution is purified from iron, zinc and cobalt. Copper sulphide cake is roasted and produced cinder is leached. Solution is directed to electro-extraction of copper, while concentrate of precious metals and chamber product are extracted from residue by flotation.

EFFECT: reduced material and operational expenditures and losses of non-ferrous and precious metals.

2 cl, 12 ex, 2 dwg

FIELD: metallurgy.

SUBSTANCE: procedure consists in processing wastes with sulphuric acid at raised temperature, in supplying hydrogen peroxide, in introducing rhenium, nickel and cobalt into leaching solution and in concentrating tungsten, niobium and tantalum in insoluble residue. Further, solution is separated from insoluble residue; extraction of rhenium from solution is leached with secondary aliphatic alcohol. Extract is washed and rhenium is re-extracted with leaching solution upon extraction. Hydrogen peroxide is supplied after main part of nickel and cobalt have passed into solution at maintaining redox potential in interval of 0.50-0.75 V relative to a saturated chlorine-silver electrode, while extraction of rhenium, extract washing and rhenium re-extraction are carried out on 2-5 steps.

EFFECT: increased extraction of rhenium at reduced consumption of oxidant, increased safety of procedure due to separated in time operations followed with release of hydrogen and oxygen.

6 cl, 4 ex

FIELD: metallurgy.

SUBSTANCE: procedure consists in underground leaching nickel with solution of sulphuric acid and in pumping product solution out. Further, acidity of product solution is reduced, and nickel is sorbed on ionite resin with its following desorption. Upon desorption raffinate of nickel sorption is made-up with sulphuric acid and directed to leaching as leaching solution. Also, excessive sulphuric acid is sorbed on separate ionite with following desorption for reduction of product solution acidity. Upon nickel sorption raffinate is made-up with sulphuric acid and with sulphuric acid after operation of its desorption.

EFFECT: simplification of process, increased ecological safety and reduced consumption of sulphuric acid.

1 dwg, 1 tbl

FIELD: metallurgy.

SUBSTANCE: processing procedure consists in supply of charge into slag melt in oxidising (melting) zone of two-zone furnace. Also charge contains source raw material and fluxes, liquid or solid processed slag, carbon containing material and oxygen containing blast supplied in quantities required for complete combustion of carbon and hydrogen with maximal heat release. Before supply of mixture of source raw material and fluxes into the oxidising (melting) zone of the furnace their mixture is preliminary roasted and supplied at temperature 500-1300C. Melted charge forms slag melt coming into a furnace zone of reduction, whereto oxygen containing blast and carbon containing material are supplied. Notably, they are supplied at amount required for reduction of extracted material into a metal phase and for compensation of heat consumption by means of after-burning gases of the reduction zone above melt, whereupon melt products are tapped.

EFFECT: raised efficiency of melting process and reduced consumption of oxygen and carbon containing material.

3 cl, 4 tbl, 5 dwg, 2 ex

FIELD: metallurgy.

SUBSTANCE: proposed method comprises dissolving wastes in acid electrolyte by applying AC electric field thereto. Dissolving is performed in nitrate or sulphate electrolyte on applying half-wave asymmetric AC industrial-frequency current and on using second electrode made from tantalum or niobium plates. Note here that anodic dissolution is carried at acidity of nitrate electrolyte at the level of 200-250 g/l HNO3, while that of sulphate electrolyte making 150-200 g/l H2SO4 at 20-40C and current of at least 1 kA.

EFFECT: increased process rate, better ecology.

3 cl, 3 tbl, 3 ex

FIELD: metallurgy.

SUBSTANCE: method involves drying of concentrate and melting in the oven. At that, melting is performed in cylindrical reaction chamber of the oven at bubbling and rotation of the molten metal with oxygen-containing jets in sulphur to oxygen ratio 1:(1-1.1). After melting is completed, the molten metal is separated into slag and matte in collector.

EFFECT: continuous high efficiency method of processing of copper-nickel sulphide concentrates so that high-grade mattes are obtained and content of cobalt in slag is decreased.

5 ex

FIELD: metallurgy.

SUBSTANCE: method consists in dissolving solubilisated components of ore by means of carrying out two or more successive stages of leaching. The first stage includes leaching at atmospheric pressure (AL), while during the second stage leaching is performed under (HPAL) pressure. In the course of this combined process average fraction of ore (0.075-0.5 mm) (1) is subjected to leaching under atmospheric pressure (AL) thereby producing flow (3) of high dissolved iron, aluminium and residual acid concentration. This said flow (3) is supplied to the next stage of leaching under pressure (HPAL) of fine fraction of ore (<0.075 mm) (4); contained free acid is re-used. Reaction of hydrolysis of iron and aluminium sulphates causes sedimentation of iron and aluminium and, thereby, regeneration of sulphuric acid.

EFFECT: reduced amount of consumed acid used for leaching.

7 cl, 4 dwg

FIELD: metallurgy.

SUBSTANCE: invention refers to procedure for processing residues of synthesis of carbonyl nickel containing non-ferrous and platinum metals. The procedure consists in charging decarbonylised residues, and in leaching in heated source hydrochloric acid solution containing not less, than 2 mole/l of nickel and cobalt chlorides and 0.25-0.5 mole/l of hydrochloric acid; also decarbonylised residues are charged discretely. Leaching is carried out with supply of gaseous chlorine and with maintaining redox potential in the interval of values 350-400 mV. Copper, iron and partially nickel and cobalt are transferred into a leaching solution. The rest part of nickel, cobalt and also platinum metals are concentrated in leaching residue. Leaching residue is processed producing concentrate of platinum metals. Produced solution of leaching is filtered, cooled and subjected to liquid extraction when a basic part of copper is recovered into extract. The basic part of copper is directed to re-extraction at presence of oxidant producing solution of copper chloride (II); further, nickel, cobalt and residual part of copper are extracted into raffinate. Also part of raffinate is directed to the leaching stage.

EFFECT: raised efficiency of processing residues of carbonyl nickel synthesis.

7 cl, 8 ex

FIELD: metallurgy.

SUBSTANCE: invention refers to procedure for processing copper-nickel mattes. The procedure consists in pouring melt of copper-nickel matte and in charging flux. Also non-ferrous scrap containing iron is charged into a source melt of copper-nickel matte. Metallised matte is produced upon blowing with oxygen containing gas mixture and upon slag tapping. Upon slag tapping metallised matte is sulphidised with reduced gases of autogenous smelting containing sulphurous anhydride to contents of sulphur equal to sulphur contents in source melt. 40-60 % of finished sulphide product is further tapped, and operations are successively repeated.

EFFECT: maintaining contents of sulphur in copper-nickel matte.

3 ex

FIELD: metallurgy.

SUBSTANCE: invention refers to hydro-metallurgy, particularly to procedure of processing silicate cobalt-nickel ore for extraction of valuable components. The procedure consists in leaching ore in acid medium with pH in the interval 1.5-2.15 at temperature 20-23C. Also leaching is performed with solution with autotrophic bacterial cultures, where amount of micro-organisms in solution equals to 105-107 cl/ml. Leaching is carried out at continuous aeration, normal atmospheric pressure and periodic replacement of solution.

EFFECT: raised level of extraction of valuable components, reduced power expenditures.

1 ex

FIELD: metallurgy, in particular complex metal recovery from oxidized ore.

SUBSTANCE: claimed method includes granulation with sulfuric acid. Obtained granules are sulfated at 250-4500C for 1-2 h in one or two steps. Then leaching of nickel and other metal sulfates are carried out followed by metal recovery using known methods. Invention is useful in reprocessing of oxidized nickel-cobalt ores, as well as laterite ores containing nickel, cobalt, and copper, and iron-manganese nickel-containing nodules.

EFFECT: high yield nickel recovery; inexpensive and usable equipment.

3 cl, 3 tbl, 4 ex

Up!